Low pressure drop reforming reactor

ABSTRACT

A syngas reforming reactor has a shell-and-tube configuration wherein the shell-side fluid flow path through the tube bundle has a longitudinal configuration. The reactor can include a shell-side inlet fluid distributor plate below the lower end of the tube bundle.

CROSS REFERENCE TO RELATED APPLICATIONS

This application is a continuation of co-pending U.S. patent applicationSer. No. 11/501,099 filed on Aug. 8, 2006, the entirety of which isincorporated by reference herein.

FIELD

The embodiments relate generally to reforming reactors for syngasproduction. As an example, the embodiments can relate to reformingreactors with a longitudinal shell-side flow configuration

BACKGROUND

Steam reforming of a hydrocarbon to manufacture syngas is a process inwhich the hydrocarbon and an oxygen source are supplied to anautothermal reformer. The combustion reaction is exothermic and suppliesthe heat needed for the catalytic reforming reaction that occurs in theautothermal reformer, which is endothermic, to produce a relatively hotreformed gas. The hot gas from the autothermal reformer is then used asa heat source in the reforming exchanger, which is operated as anendothermic catalytic steam reforming zone. In the reforming exchanger,a feed comprising a mixture of steam and hydrocarbon is passed throughcatalyst-filled tubes. The outlet ends of the tubes discharge theendothermically reformed gas near the shell side inlet where it mixeswith the hot gas from the autothermal reformer. The hot gas mixture isthen passed countercurrently across the tubes in indirect heat exchangeto supply the heat necessary for the endothermic reforming reaction tooccur.

Reforming exchangers are in use commercially and are available. Variousimprovements to the reforming exchanger design have included, forexample, the tube bundle support and low pressure drop tubes.

A need exists for improving the basic reforming exchanger design tominimize the capital cost of the equipment. Current reforming exchangerdesign uses expensive alloys in the construction the tube bundle andtube sheets since the reforming exchanger are used at relatively highoperating temperatures and pressures.

A need exists for improving the basic reforming exchanger design tomaximize the capacity of the reforming exchanger within the practicallimits of fabrication capabilities. Further, if the size and weight ofthe reforming exchanger is minimized, maintenance operations thatrequire removal of the tube bundle will be facilitated.

One approach to reducing the capital cost and increasing the capacity ofthe reforming exchanger is to increase the ratio of surface area tovolume of the reactor tubes. By decreasing diameter of the tubes andusing monolithic catalyst structures in the reforming exchanger design,the capital costs are decreased and/or the capacity is increased withrespect to the tube bundle.

A need for similar improvements to the shell-side of the reformingexchanger, especially improvements that can maintain and improve theadvantages of the small-diameter tubes. Previous designs have usuallyutilized a minimum of five shell-side cross passes with no tubes in thebaffle windows. Five cross-flow passes in tube bundles can result in anexcessive shell-side pressure drop in some instances. While fewer passescan be used to reduce the shell-side pressure drop, the resultingreforming kinetics could be uneven due to an uneven shell-sidetemperature profile.

BRIEF DESCRIPTION OF THE DRAWINGS

The detailed description will be better understood in conjunction withthe accompanying drawings as follows:

FIG. 1 depicts cross-sectional side elevation of an embodiment of areforming reactor.

FIG. 2 depicts a cross-sectional view of the embodiment of a reformingreactor as exampled in FIG. 1 as seen along the lines 2-2 showing thedischarge flow annulus.

FIG. 3 depicts a cross-sectional view of the embodiment of a reformingreactor as exampled in FIG. 1 as seen along the lines 3-3 showing alattice support assembly.

FIG. 4 depicts a velocity vector diagram of a comparative reformingreactor with the embodiments exampled in FIG. 1, FIG. 2, and FIG. 3, butwithout the shell-side inlet distributor, shown in vertical section.

FIG. 5 depicts a longitudinal direction velocity diagram of acomparative reforming reactor with the embodiments exampled in FIG. 1,FIG. 2, and FIG. 3, but without the shell-side inlet distributor, shownin vertical section.

FIG. 6 depicts a velocity vector diagram of a reforming reactor withembodiments exampled in FIG. 1, FIG. 2, and FIG. 3 with a shell-sideinlet distributor, shown in vertical section.

FIG. 7 depicts a longitudinal direction velocity diagram of a reformingreactor with embodiments exampled in FIG. 1, FIG. 2, and FIG. 3 with ashell-side inlet distributor 123, shown in vertical section.

The embodiments are detailed below with reference to the listed Figures.

DETAILED DESCRIPTION OF THE EMBODIMENTS

Before explaining the embodiments in detail, it is to be understood thatthe embodiments are not limited to the particular embodiments and thatthey can be practiced or carried out in various ways.

An embodiment of a reforming exchanger design uses a shell-side flowarrangement that provides a longitudinal countercurrent flow through thetube bundle. A longitudinal shell-side flow arrangement can result inefficient heat transfer with a low pressure drop in the shell-sidefluid. The longitudinal shell-side flow arrangement benefits from inletand outlet flow distributors that eliminate the tube-free flow windowsutilized on either side of the cross-flow baffles of the conventionalprior art cross-flow reforming reactor designs. The longitudinalshell-side flow arrangement can result in a less costly reactor designsince the longitudinal shell-side flow arrangement has a relativelysmaller shell diameter compared to the prior art cross-flow design.

In an embodiment, a syngas reforming exchanger is provided in the formof a vessel with an elongated shell having relatively high and lowtemperature ends. A shell side fluid inlet is adjacent to the hightemperature end of the reforming exchanger. The shell side fluid inletallows a hot gas feed to enter the reforming exchanger. A tube sidefluid inlet is adjacent to the low temperature end of the reformingexchanger. The tube side fluid inlet allows a reactant feed gas to enterthe reforming exchanger. A shell side fluid outlet is fluidly isolatedfrom the tube side fluid inlet by a tube sheet. The shell side fluidoutlet is adjacent to the low temperature end of the reforming exchangerand allows the cooled gas to be discharged from the reforming exchanger.

A tube bundle can include one or more tubes, one or morelongitudinally-spaced transverse ring baffles, and one or morelongitudinally-spaced tube guides. The tubes have an inlet end securedto the tube sheet, and an outlet end located adjacent to the shell sidefluid inlet. The gas mixture follows a longitudinal shell-side flow paththrough the tube bundle. A heat resistant refractory lining can beaffixed to an interior surface of the shell about the tube bundle.

A discharge annulus is defined between a flow sleeve disposed about thetube bundle and an enlarged end of the shell adjacent the shell-sidefluid outlet, and in fluid communication between the shell-side flowpath and the shell-side fluid outlet. The flow sleeve has open end and asealed end. The open end is spaced from the tube sheet in communicationwith the shell-side fluid outlet; the sealed end forms a seal with theshell refractory lining at a base of the discharge annulus.

In an embodiment, the reactant gas includes hydrocarbon and steam; theproduct gas includes reformed gas. The reactor can includecatalyst-bearing monolithic structures disposed within the tubes forconverting the gas feed mixture to reformed gas. In an embodiment, thetubes have an inside diameter that is not more than 4 times a maximumedge dimension of the catalyst structures.

In an embodiment, the syngas reforming exchanger includes a flangeassembly adjacent to the low temperature end. The tube sheet can besecured to a tube sheet using a support member. An example supportmember can include an annular lip mounted in the flange assembly, and askirt that extends from and is secured to the lip at one end and securedto the tube sheet at an opposite end. A tube sheet refractory lining canbe located on a shell-side face of the tube sheet, and/or a skirtrefractory lining can be located on an inside face of the skirtextending from adjacent the lip to the tube sheet. The syngas reformingexchanger can include a seal between the tube sheet refractory liningand an upper end of the shell refractory lining to inhibit shell sidefluid entry into an annulus between the skirt and an inner wall of thevessel. As an example, the tube sheet refractory lining can be surfacedwith a high temperature, erosion-resistant cap. The tube bundle can beremovable from the shell.

In an embodiment, a flow distributor (for example, a perforatedtransverse plate) can be disposed between the shell-side fluid inlet andthe tube bundle.

In an embodiment, one of the ring baffles can be disposed in the flowsleeve adjacent the open end thereof. The tube bundle can include one ormore ring baffles (for example from 3 to 6 ring baffles in oneembodiment). The ring baffles can have a central flow window, wherein aportion of the tubes pass through the window, and another portion canpass through an annular plate of the baffle.

In an embodiment, the tube guides are in the form of transverse latticesupport assemblies, which can include first and second sets of parallellattice support bars adjacent a common plane and extending between thetubes with opposite ends of the support bars secured to a latticesupport ring. The parallel lattice support bars in the first set aretransverse to the parallel lattice support bars in the second set. Thelattice support ring can include an annular plate extending inwardlyfrom an end of a cylindrical section (for example, one of the ringbaffles can extend inwardly from an end of a cylindrical section). Thetube bundle can have tie rods to maintain the lattice support assembliesin longitudinal displacement with respect to the tube sheet.

In an embodiment, the seal between the shell refractory lining and thedischarge annulus can be formed by a base ring extending outwardly fromthe flow sleeve, and a seal between the base ring and a transverseannular surface formed in shell refractory lining at the base of thedischarge annulus.

In an embodiment, the tubes can have an Lt/Dt ratio of at least 180,wherein Lt is taken as the length of the catalyst bearing extent of thetubes and Dt is the inside diameter of the tubes. In variousembodiments, the catalyst-bearing monolithic structures are in the formof a twisted tape insert, a central longitudinal runner and a pluralityof bristles extending transversely therefrom, ceramic foam, Raschigrings, or the like.

The countercurrent flow arrangement can be characterized by an effectivelogarithmic mean temperature difference correction factor of at least0.95, at least 0.98, at least 0.99, or at least 0.995, or essentially 1.

In another embodiment, the invention provides a method of reforming ahydrocarbon with steam with the reforming exchanger described above. Themethod includes the steps of supplying a mixture of preheatedhydrocarbon and steam to the tube-side inlet of the reforming exchanger,supplying a relatively hot gas to the shell-side inlet, and withdrawinga reformed gas from the shell-side outlet.

With reference to the figures, FIG. 1 depicts cross-sectional sideelevation of an embodiment of a reforming reactor. FIG. 2 depicts across-sectional view of the embodiment of a reforming reactor asexampled in FIG. 1 as seen along the lines 2-2 showing the dischargeflow annulus. FIG. 3 depicts a cross-sectional view of the embodiment ofa reforming reactor as exampled in FIG. 1 as seen along the lines 3-3showing a lattice support assembly. The exampled reforming exchanger 100in the noted figures has a tube side fluid inlet 102, a shell side fluidinlet 104, and a shell side fluid outlet 106 in an elongated shell 108.The exampled reforming exchanger 100 has respective relatively high andlow temperature ends 110 and 112. As used herein, the term“longitudinal” refers to the direction corresponding to the length ofthe reforming exchanger 100 or generally parallel to the longitudinalaxis, whereas “transverse” means transverse with respect to thelongitudinal axis unless otherwise indicated.

The shell side fluid inlet 104 is adjacent to the high temperature end110 for receiving a hot gas feed. The shell side fluid outlet 106 isadjacent to the low temperature end 112 for discharging cooled gas fromthe reforming exchanger 100. The tube side fluid inlet 102 is adjacentto the low temperature end 112 for receiving a feed mixture ofhydrocarbon and steam. The tube side fluid inlet 102 is fluidly isolatedfrom the shell side fluid outlet 106 by tube sheet 114 from which tubebundle 116 is supported. The terms “upper” and “lower” may be used forconvenience to correspond to the directions toward the tube-side inlet102/shell-side outlet 106/low temperature end 112 and toward theshell-side inlet 104/high temperature end 110, respectively, althoughthere is no requirement for such a vertical orientation of the exchanger100.

In the exampled reforming exchanger 100, a flow sleeve 118 is disposedabout the tube bundle 116 adjacent to the shell side fluid outlet 106. Adischarge annulus 120 is between an outer surface of the imperforateflow sleeve 118 and an enlarged diameter region of the shell 108. Theflow sleeve 118 has an open end spaced from the tube sheet 114, and issealed at an opposite end adjacent to a base of the discharge annulus120.

In operation, relatively cool reactant feed fluid (for example, fluidranging from about 480° to about 760° C.) enters inlet 102. The reactantfeed flows downward through tube sheet 114 and the tube bundle 116. Thetube bundle 116 includes a plurality (in some embodiments severalhundred up to a thousand or more) of catalyst-filled tubes 122 in whichthe reactants are catalytically reacted. The reacted fluid leaves thelower end of each tube 122. A heating fluid (for example, effluent froma reformer, such as a fired tubular or non-tubular reformer) isintroduced in shell side inlet 104, passed through perforations in adistributor plate 123, and distributed to mix with the reacted fluid.The mixture of the reacted fluid and heating fluid flows longitudinallythrough the tube bundle 116 for generally true countercurrent heattransfer (the logarithmic mean temperature difference correction factoris essentially 1.0 within a 0.5-5% tolerance range) with the tubes 122.The cooled mixture exits the tube bundle 116 from the open end of theflow sleeve 118, through the discharge annulus 120, and is dischargedthrough the shell side fluid outlet 106 for further processing in aconventional manner.

A tube-side inlet chamber 124 can be enclosed by a head 126 secured toshell 108 by flange assembly 128. The tube sheet 114 serves as apartition to isolate fluid in the chamber 124 from fluid in the shell108. The exchanger 100 can include a heat-resistant refractory lining130 affixed to the interior surfaces of the chamber 124 and shell 108.The refractory lining can be composed of ceramic or cement-likematerials well known in the art and can include one or more layers. Forexample, the refractory lining can have a high density inner layer 130-1(as exampled in FIG. 2 and FIG. 3) exposed to the interior of the shell108 and/or chamber 124, and a backup or insulating layer 130-2positioned between the inner layer 130-1 and the respective innersurface of the shell 108 and/or chamber 124. This refractory can beassembled using conventional refractory anchors, cold seams, andmounting hardware generally used for this purpose in the art.

The operating temperatures for which the exchanger 100 is designed canvary from approximately 400° C. to approximately 650° C. (752° F. and1202° F.) for the components in the tube-side chamber 124, and fromapproximately 650° C. to approximately 1050° C. (1202° F. and 1922° F.)for components in the shell 108. The exchanger 100 can withstandinternal pressures up to pressures from approximately 2.4 MPa toapproximately 6.9 MPa (350-1000 psi). A conventional water/steam jacket132 can be used to monitor for generation of greater-than-normal amountsof steam which may indicate a potential “hot spot” or refractoryfailure.

The tube sheet 114 can be constructed from various types of heatresistant steel plate known in the art, and is preferably supported froma generally cylindrical skirt 134 with a lip 136 for engagement with theflange assembly 128. Refractory linings can be provided at an insidesurface of the skirt 134 and a shell-side surface of the tube sheet 114,and these can be provided with a respective erosion-resistant cap 133-1,133-2, which can be made from a high temperature alloy sheet.

The tube bundle 116 can made up of the tubes 122, one or more ringbaffles 138 (also known as donut baffles), and one or more latticesupport assemblies 140 (also known as rod or grid baffles). Eachindividual tube 122 can be expanded and/or strength welded to the tubesheet 114. The tube sheet 114 serves to support and position the tubebundle 116, as well as lattice support assemblies 140, baffles 138, andthe distributor plate 123, in conjunction with a plurality of tie rods125 which are threaded into the tube sheet 114 and extend to stabilizethe support assemblies 140 and baffles 138 against spacer tubes 125-1and washers 125-2.

As exampled in FIG. 2, the baffles 138 can be in the form of an annularplate that can be perforated to slideably receive outermost ones 122-1of the individual tubes. The baffles 138 alternatively or additionallycan have an inner contour to match a profile of outermost and/orpenultimately outermost ones 122-2 of the tubes. The baffles 138 canhave an outside diameter that, taking thermal expansion into account,matches an inside diameter of the refractory 130 (as exampled in FIG. 1)to facilitate insertion and removal of the modular tube bundle 116. Forexample, at ambient temperatures the baffles 138 have sufficientclearance with the refractory 130 to allow the tube bundle 116 to bemoved or slid in or out of engagement with the refractory, but atoperating temperature the baffles 138 have an outside diameter that isnearly equal to the inside diameter of the refractory 130 to inhibitfluid bypass around the outside of the tube bundle 116. The innercontour defines a generally circular flow window 142 for shell-sidefluid to flow longitudinally through the tubes 122 within the flowwindow 142. The baffles 138 can facilitate turbulence and mixing in theshell side fluid to promote a more even shell-side fluid temperature andimprove uniformity of heat transfer. As an example, 3 to 6 or more ringbaffles 138 can be employed, but the number is not critical and more orfewer can be used.

As exampled in FIG. 1 and FIG. 3, the lattice support assemblies 140 caninclude first parallel lattice supports 144, and second parallel latticesupports 146 that are transverse to the first lateral supports 144. Thelattice supports 144, 146 can be in the form of rectangular bars with athickness corresponding to a spacing between the tubes 122 and length tospan between opposite sides of a support ring 148. In the case oftriangular pitch tubes 122, the first and second lattice supports 144,146 can be oriented with an angular offset about 30 degrees fromperpendicular with respect to each other (for example, with a largeangle of about 120 degrees and a small angle of about 60 degrees).

The support ring 148 can be welded or otherwise secured to the ends ofthe lattice supports 144, 146. In one embodiment, the lattice supports144, 146 are stacked longitudinally in abutment and the length or heightof the support ring 148 corresponds to the total height of the latticesupports 144, 146. If desired, the support ring 148 and/or the latticesupports 146 (or alternatively or additionally lattice supports 144) canbe secured to one of the baffles 138 for additional strength and tofacilitate longitudinal positioning of the lattice support assembly 140via tie rods 125.

The lattice support assembly 140 serves to maintain spacing and pitch ofthe tubes 122, and can also facilitate abatement of any vibration. Inaddition, the lattice support assembly 140 promotes turbulence andthermal mixing of the shell-side fluid as it passes between and aroundthe lattice supports 144, 146, which facilitate a larger temperaturedifferential at the surfaces of the tubes 122 and improve the overallrate and uniformity of the heat transfer.

The support ring 148 can have an outside diameter matching the insidediameter of the refractory 130 in the main part of the shell 108, takingany differential thermal expansion into account, to facilitate insertionand removal of the tube bundle 116, for example, in the hot or operatingcondition there can be a radial gap of about 3 mm (0.125 in.) betweenthe support ring 148 and refractory 130. In an embodiment, the supportring 148, in one or more of any lattice support assemblies 140 that areadjacent the discharge annulus 120, has an outside diameter matching aninside diameter of the flow sleeve 118 for attachment thereto by weldingor other conventional means. The flow sleeve 118 and support ring 148can be made of the same material or, if different, materials withcompatible thermal expansion coefficients. The flow sleeve 118 ispositioned on the tube bundle 116 so that the upper end is evenly spacedfrom the tube sheet 114 and/or its refractory lining so as to define aradial slot for generally uniform passage of the shell-side fluid fromthe tube bundle 116 into the discharge annulus 120.

The flow sleeve 118 can be secured to an outwardly extending base ring150 adjacent a lower end opposite the tube sheet 114. The base ring 150can have a surface opposite the discharge annulus 120 supporting a flowseal 152, such as a conventional resilient high temperature ceramicmaterial that is designed for compression, e.g. from 24 mm to 12 mm inone embodiment. Such gaskets are can be made, for example, fromspot-welded 28 BWG tp 347 sheet metal backing filled with 24 mm SAFFIL®95% alumina low density mat. A transverse annular sealing surface isformed in an upper end the refractory lining 130, possibly within thedense layer 130-1, for sealing engagement with the gasket and base ring150, conveniently in a transition region at the base of the dischargeannulus where the diameter of the shell changes.

The flow sleeve 118 serves to direct shell-side fluid longitudinallyover the upper ends of the tubes 122 to prevent short-circuiting offluid to the shell-side outlet 106 which would otherwise result inuneven heat transfer with the tubes 122. A perfect fluid-tight seal isthus not absolutely necessary, and some limited fluid leakage at seal152 can be tolerated.

A similar flow seal 154 can be employed between the tube sheet cap 133-2and a transverse annular surface at an upper end of the refractory 130adjacent the discharge annulus 120 to facilitate maintaining the lip 136and flange assembly 128 at a relatively low temperature. If desired, adeflection ring 156 can project from the cap 133-2 adjacent the seal 154to protect the seal 154 from wash-out that might otherwise result fromimpingement by the shell-side fluid into the discharge annulus 120.

The tubes 122 can have a ratio of Lt/Dt of at least 180, at least 200,at least 250, at least 300, or at least 300-400. In determining Lt/Dt,the diameter Dt refers to the inside diameter of the tubes 122 in thecase of right circular cylindrical tubes, or to the equivalent hydraulicdiameter in the case of non-circular tubes. The length Lt refers to thecatalyst-filled or -packed length. Higher Lt/Dt ratios are preferred inthe embodiments because the heat transfer coefficients are generallyhigher than with a lower Lt/Dt ratio, and the resulting equipment costis lower. A longer, smaller-ID catalyst tube 122 can result in moretubes 122 in the tube bundle 116, but the tube bundle 116 can have asmaller diameter for a given conversion capacity, allowing the use of ashell 108 that has a smaller diameter. The reduction of the diameter ofthe shell 108 and tube bundle 116 can result in more capital costsavings than result from any increase in the length thereof, and thusthe reforming exchanger 100 of the present invention can be much cheaperto fabricate than a prior art reforming exchanger of equivalentcapacity. This result is advantageous in the design of a new reformingexchanger 100.

If the same shell diameters and tube lengths of a prior art reformingexchanger are used so that the capital costs thereof are substantiallyequivalent, the conversion capacity of the reforming exchanger 100 issubstantially increased. This latter result is advantageous in thereplacement of existing reforming exchangers so that the new reformingexchanger 100 has about the same size but with a higher capacity thanthe original reforming exchanger it replaced.

In the embodiments, the ratio of the tube inside diameter (ID), Dt, tothe largest edge dimension of the catalyst structure (Dp) can berelatively small compared to the same ratio in conventional reformingexchangers, as exampled in Burlingame U.S. Pat. No. 6,855,2721. Forexample, in prior art reforming exchangers employing Raschig ringcatalyst measuring 8 mm (0.31-in.) OD by 3 mm (0.125-in.) ID by 8 mm(0.31-in.) long, the minimum tube ID was about 50.8 mm (2 in.). In theBurlingame design, the same Raschig ring catalyst can be used inapproximately 32 mm (1.25-in.) or even 25 mm (1-in.) ID tubes with anequivalent or slightly higher ratio of heat transfer to pressure drop.In Burlingame design, the Dt/Dp ratio is preferably not more than 4, andmore preferably about 3 or less.

A low delta P catalyst structure is defined herein as any suitablecatalyst structure that results in a higher rate of heat transfer perunit of tube side pressure drop than in 50.8 mm (2-in.) ID reformingexchanger tubes filled with catalyst-supporting Raschig rings measuring8 mm (0.31-in.) OD by 3 mm (0.125-in.) ID by 8 mm (0.31-in.) long undersimilar operating conditions and conversions.

Several different types of low delta P monolithic catalyst supportstructures are disclosed in Burlingame et al. While the low delta P isan important property, the Burlingame et al. catalysts are alsotypically found to have a relatively high void fraction and present atortuous flow path to the tube side fluid. Catalyst activity can berelatively low to moderate without significant reduction in conversionrates, although there is no general detriment to using a high activitycatalyst aside from the typically higher cost involved.

In an embodiment, the skirt 134 can be constructed of differentmaterials to facilitate reducing thermal stresses which could develop inservice. The tube sheet 114 is generally made of a high temperaturealloy (for example, 304H stainless steel) with a relatively high thermalexpansion coefficient. A lower portion of the skirt 134 can be made ofthe same or a similar high temperature alloy welded directly to the tubesheet 114. The lip 136 and an upper portion of the skirt 134 can be madeof materials, which can be the same or different, suited for relativelycooler temperatures (for example, 1¼% chromium-½% molybdenum steelalloy) generally having a relatively lower thermal expansioncoefficient. An intermediate portion of the skirt 134 can be made from amaterial having an intermediate thermal expansion coefficient (forexample, INCONEL chromium-nickel alloy) to help relieve the thermalstresses which could otherwise develop if the skirt 134 were made fromonly one or two materials.

The lip 136 can be provided with a plurality of threaded bores (notshown) by which the entire assembly of the skirt 134, the tube sheet 114and the tube bundle 116 are conventionally hoisted for pulling orreplacement when this is necessary, for example, by threading eye boltsinto the bores and passing a suitable cable from a crane, wench, hoistor the like through the eyes. The base ring 150 has an outside diameterthat is less than the outside diameter of the discharge annulus 120 sothat the base ring 150 can clear the refractory 132 during insertion ofthe tube bundle 116. Similarly, the tube sheet 114 and skirt 134 have anoutside diameter less than the inside diameter of the cylindricalportion of the chamber 124 below the flange assembly 128.

With the flange assembly 128 disengaged and the head 126 removed, thepreassembled tube sheet 114, tube bundle 116, and skirt 134, can behoisted above the shell 108 and lowered in place for the base ring 150and seal 152 to engage (at operating temperature) with the refractory132 at the lower end of the discharge annulus 120, for the cap 133-2 andseal 154 to engage (at operating temperature) with the refractory 132 atthe lower end of the discharge annulus 120, and for the lip 136 toengage with the lower flange of the flange assembly 128.

A distributor plate 123 can be positioned below the tube bundle 116 andsecured to the tube sheet 114 by the tie rods 125 and nuts 125-1. Thedistributor plate 123 has an outside diameter matching an insidediameter of the refractory 130, and is perforated to assure uniformdistribution of the flow of the process gas from the shell-side fluidinlet 104. The size, number and shape of the perforations are selectedto provide the desired flow distribution at the expected operatingconditions. A series of distributor plates may be used if required foradequate flow distribution.

FIG. 4 depicts a velocity vector diagram of a comparative reformingreactor with the embodiments exampled in FIG. 1, FIG. 2, and FIG. 3, butwithout the shell-side inlet distributor, shown in vertical section.FIG. 5 depicts a longitudinal direction velocity diagram of acomparative reforming reactor with the embodiments exampled in FIG. 1,FIG. 2, and FIG. 3, but without the shell-side inlet distributor, shownin vertical section. FIG. 6 depicts a velocity vector diagram of areforming reactor with embodiments exampled in FIG. 1, FIG. 2, and FIG.3 with a shell-side inlet distributor, shown in vertical section. FIG. 7depicts a longitudinal direction velocity diagram of a reforming reactorwith embodiments exampled in FIG. 1, FIG. 2, and FIG. 3 with ashell-side inlet distributor 123, shown in vertical section.

For comparison purposes, FIG. 4 and FIG. 5 illustrate the flowarrangement without the distributor plate 123, and FIG. 6 and FIG. 7illustrate the flow arrangement with the distributor plate present witha pressure drop of approximately 3.45 kPa (0.5 psi). The flowdistributions seen in FIGS. 4 through 7 were developed using acomputational fluid dynamic (CFD) model based on a simplifiedarrangement without the tube bundle 116. FIG. 6 and FIG. 7 show thatsignificant improvement in the uniformity of the flow is achieved, andeven better distribution can be expected if the tube bundle 116 weretaken into account in the model.

EXAMPLES

Design parameters for a longitudinal flow reforming reactor 100according to the present invention (Example 1) was developed as theresult of a conceptual sizing review and compared to 3-, 4- and 5-passcross flow reforming reactors (Comparative Examples 1-3). The designbasis included tubes with an OD of 28.575 mm (1.125 in.) and a maximumshell-side pressure drop of 50 kg/cm2 (7.25 psi). The design parametersand relative capital costs are summarized in Table 1 below.

TABLE 1 TABLE 1 Comp. Comp. Comp. Parameter Example 1 Example 1 Example2 Example 3 Shell-side flow longitudinal 3-pass cross 4-pass cross5-pass cross configuration flow flow flow Refractory ID, mm (in.) 1265(50) 1549 (61) 1778 (70) 2032 (80) Shell ID, mm (in.) 1620 (64) 1905(75) 2134 (84) 2388 (94) Tube length mm (ft) 5600 (18.37) 5258 (17.25)5639 (18.5) 6096 (20) Number of tubes 927    843    875   916   Relativesurface 447 (4811) 381 (4101) 425 (4575) 483 (5200) area m2 (ft2) Shellside ΔP, 0.49 (6.97) 0.47 (6.69) 0.47 (6.69) 0.51 (7.25) kg/cm2 (psi)Shell-side 439 (90) 1592 (326) 1421 (291) 1352 (277) coefficient,kcal/h- m2-C (Btu/hr-ft²-° F.) Excess surface, % 8.5 6.6 20.1 37.9Estimated cost Base = 1.0  1.09  1.27  1.48 (relative)

These results show that the shell and refractory inside diameters aresignificantly less with a longitudinal shell-side flow configurationthan with a cross-flow configuration. The estimated cost of thelongitudinal flow reactor (Example 1) is lower than the cross flowreactors (Comp. Examples 1-3). The capital cost is substantially loweredfor the case of the longitudinal flow reactor of Example 1, oralternatively the shell-side pressure drop could be significantly lowerfor the same capital cost.

All patent references and publications referred to above are herebyincorporated herein by reference in their entirety for the purpose of USpatent prosecution and other jurisdictions where permitted.

While these embodiments have been described with emphasis on theembodiments, it should be understood that within the scope of theappended claims, the embodiments might be practiced other than asspecifically described herein.

1. A syngas reforming exchanger comprising: a vessel comprising anelongated shell having relatively high and low temperature ends; a shellside fluid inlet adjacent the high temperature end for receiving a hotgas feed; a tube side fluid inlet adjacent the low temperature end forreceiving a reactant feed gas; a shell side fluid outlet fluidlyisolated from the tube side fluid inlet by a tube sheet adjacent the lowtemperature end for discharging cooled gas; a tube bundle comprising aplurality of tubes, wherein the tubes have an inlet end secured to thetube sheet for receiving the feed mixture and an outlet end adjacent theshell side fluid inlet for discharging product gas into the hot gas feedto form a gas mixture; a longitudinal shell-side flow path for the gasmixture through the tube bundle; a heat resistant refractory liningaffixed to an interior surface of the shell about the tube bundle; animperforate sleeve at least partially disposed about the tube bundle fordirecting the gas mixture over the inlet ends of the tubes; and adischarge annulus defined between the sleeve and the shell slide fluidoutlet.
 2. The syngas reforming exchanger of claim 1, further comprisingcatalyst-bearing monolithic structures disposed within the tubes forconverting the gas feed mixture to reformed gas, wherein the tubes havean inside diameter that is not more than 4 times a maximum edgedimension of the catalyst structures.
 3. The syngas reforming exchangerof claim 2, wherein the catalyst-bearing monolithic structures comprisea member selected from the group consisting of a twisted tape insert;ceramic foam; Raschig rings; and central longitudinal runner and aplurality of bristles extending transversely therefrom.
 4. The syngasreforming exchanger of claim 2, wherein the catalyst-bearing monolithicstructures comprise a twisted tape insert with a wash-coated surfaceimpregnated with a nickel-containing catalyst.
 5. The syngas reformingexchanger of claim 2, wherein the catalyst-bearing monolithic structurescomprise a central longitudinal runner, a plurality of bristlesextending transversely therefrom and the bristles are wash-coated andimpregnated with a nickel-containing catalyst.
 6. The syngas reformingexchanger of claim 1, further comprising: a flange assembly adjacent thelow temperature end; wherein the tube sheet is secured to a tube sheetsupport member comprising an annular lip mounted in the flange assemblyand a skirt extending from and secured to the lip at one end and securedto the tube sheet at an opposite end; a tube sheet refractory lining ona shell-side face of the tube sheet; a skirt refractory lining on aninside face of the skirt extending from adjacent the lip to the tubesheet.
 7. The syngas reforming exchanger of claim 6, further comprisinga seal between the tube sheet refractory lining and an upper end of theshell refractory lining to inhibit shell side fluid entry into anannulus between the skirt and an inner wall of the vessel.
 8. The syngasreforming exchanger of claim 7, wherein the tube sheet refractory liningis surfaced with a high temperature, erosion-resistant cap.
 9. Thesyngas reforming exchanger of claim 1, further comprising a flowdistributor disposed between the shell-side fluid inlet and the tubebundle.
 10. The syngas reforming exchanger of claim 9, wherein the flowdistributor comprises a perforated transverse plate.
 11. The syngasreforming exchanger of claim 1, wherein the tubes have an Lt/Dt ratio ofat least 300, wherein Lt is taken as the length of the catalyst bearingextent of the tubes and Dt is the inside diameter of the tubes.
 12. Asyngas reforming exchanger comprising: a vessel comprising an elongatedshell having relatively high and low temperature ends; a shell sidefluid inlet adjacent the high temperature end for receiving a hot gasfeed; a tube side fluid inlet adjacent the low temperature end forreceiving a reactant feed gas; a shell side fluid outlet fluidlyisolated from the tube side fluid inlet by a tube sheet adjacent the lowtemperature end for discharging cooled gas; a tube bundle comprising aplurality of tubes, wherein the tubes have an inlet end secured to thetube sheet for receiving the feed mixture and an outlet end adjacent theshell side fluid inlet for discharging product gas into the hot gas feedto form a gas mixture, and one or more lattice support assemblies formaintaining spacing and pitch of the plurality of tubes; a longitudinalshell-side flow path for the gas mixture through the tube bundle; a heatresistant refractory lining affixed to an interior surface of the shellabout the tube bundle; an imperforate sleeve disposed at least partiallyabout the tube bundle for directing the gas mixture over the inlet endsof the tubes; and a discharge annulus defined between the sleeve and theshell slide fluid outlet.